Process for the coversion of synthesis gas to oxygenates

ABSTRACT

The present invention relates to an improved process for the conversion of carbon oxide(s) and hydrogen containing feedstocks to oxygen containing hydrocarbon compounds in the presence of a particulate catalyst. In particular, the present invention relates to an improved process for the conversion of carbon oxide(s) (CO and CO2) and hydrogen containing feedstocks, e.g. synthesis gas or syngas, to alcohols in the presence of a particulate modified molybdenum sulphide based catalyst, or a modified methanol based catalyst and/or a modified Fischer-Tropsch catalyst and/or a precious metal (e.g. rhodium) based catalyst.

The present invention relates to an improved process for the conversionof carbon oxide(s) and hydrogen containing feedstocks to oxygencontaining hydrocarbon compounds in the presence of a particulatecatalyst.

In particular, the present invention relates to an improved process forthe conversion of carbon oxide(s) (CO and CO2) and hydrogen containingfeedstocks, e.g. synthesis gas or syngas, to alcohols in the presence ofa particulate modified molybdenum sulphide based catalyst, and/or amodified methanol based catalyst and/or a modified Fischer-Tropschcatalyst and/or a precious metal based catalyst, such as rhodium.

U.S. Pat. No. 4,122,110 relates to a process for manufacturing alcohols,particularly linear saturated primary alcohols, by reacting carbonmonoxide with hydrogen at a pressure between 20 and 250 bars and atemperature between 150° C. and 400° C., in the presence of a catalyst,characterized in that the catalyst contains at least 4 essentialcomponents: (a) copper (b) cobalt (c) at least one element M selectedfrom chromium, iron, vanadium and manganese, and (d) at least one alkalimetal.

U.S. Pat. No. 4,831,060 relates to the production of mixed alcohols fromcarbon monoxide and hydrogen gases using a catalyst, with optionally aco-catalyst, wherein the catalyst metals are molybdenum, tungsten orrhenium, and the co-catalyst metals are cobalt, nickel or iron.

The catalyst is promoted with a Fischer-Tropsch promoter like an alkalior alkaline earth series metal or a smaller amount of thorium and isfurther treated by sulfiding. The composition of the mixed alcoholsfraction can be selected by selecting the extent of intimate contactamong the catalytic components.

Journal of Catalysis 114, 90-99 (1988) discloses a mechanism of ethanolformation from synthesis gas over CuO/ZnO/Al2O3. The formation ofethanol from CO and H2 over a CuO/ZnO methanol catalyst is studied in afixed-bed microreactor by measuring the isotopic distribution of thecarbon in the product ethanol when C(13) methanol was added to the feed.

It is an object of the present invention to provide an improved processin terms of selectivity and catalyst activity and operating life for theconversion of carbon oxide(s) and hydrogen containing feedstocks tooxygen containing hydrocarbon compounds in the presence of a particulatecatalyst. Where, a particulate catalyst is defined as being either asupported or unsupported heterogeneous catalyst.

In particular, the present invention relates to an improved process interms of selectivity and catalyst activity and operating life, for theconversion of carbon oxide(s) and hydrogen containing feedstocks, e.g.synthesis gas or syngas, to alcohols in the presence of a particulatecatalyst; whereby the said particulate catalyst may comprise any one ormore of the following: a modified molybdenum sulphide based catalyst;and/or a modified methanol based catalyst; and/or a modifiedFischer-Tropsch catalyst; and/or a precious metal based catalyst, suchas rhodium.

The present invention thus provides a process for the conversion ofcarbon oxide(s) and hydrogen containing feedstocks to oxygen containinghydrocarbon compounds in the presence of a particulate catalyst,comprising the step of reacting carbon oxide(s) and hydrogen in thepresence of a particulate catalyst in a conversion reactor to formproducts comprising oxygen containing hydrocarbon compounds;characterised in that ether(s) are added and reacted inside theconversion reactor.

In particular, the present invention provides a process for theconversion of carbon oxide(s) and hydrogen containing feedstocks, e.g.synthesis gas or syngas, to alcohols in the presence of a particulatemodified molybdenum sulphide based catalyst and/or a modified methanolbased catalyst and/or a modified Fischer-Tropsch catalyst and/or aprecious metal based catalyst (e.g. rhodium), comprising the step ofreacting carbon monoxide and hydrogen in the presence of said catalystin a conversion reactor to form alcohols characterised in that an etheris added and reacted inside the conversion reactor.

According to a preferred embodiment, the present invention provides aprocess for the conversion of hydrocarbon to alcohols comprising thesteps of:

1. converting a hydrocarbon feedstock into a mixture of carbon oxide(s)and hydrogen in a syngas reactor,

2. passing the mixture of carbon oxide(s) and hydrogen from the syngasreactor to a conversion reactor, and

3. reacting said mixture in said conversion reactor in the presence of aparticulate modified molybdenum sulphide based catalyst and/or amodified methanol based catalyst and/or a modified Fischer-Tropschcatalyst and/or a precious metal based catalyst (e.g. rhodium) to formalcohols,

characterised in that an ether(s) is added and reacted inside theconversion reactor.

For the purpose of the present invention and appending claims,“producing oxygen containing hydrocarbon compounds from a mixture ofcarbon oxide(s) and hydrogen (e.g. synthesis gas)”, means that theoxygen containing hydrocarbons (oxygenates) represent at least 10% byweight, preferably at least 20% by weight, preferably at least 40% byweight, preferably at least 70% by weight and most preferably at least90% by weight of the total liquid (under STP conditions) productsexiting the conversion reactor.

According to a preferred embodiment of the present invention, the oxygencontaining hydrocarbon compounds are alcohols and other organicoxygenates, such as ethers.

According to a further embodiment of the present invention, the alcoholscomprise mainly methanol, ethanol, propanols (predominately n-propanolwith low amounts of isopropanol) and butanols (predominately n-butanoland isobutanol); said methanol, ethanol, propanols and butanolspreferably represent together at least 5% by weight, more preferably atleast 10% by weight and most preferably at least 20% by weight of thetotal liquid (under STP conditions) products exiting the conversionreactor. The ethers may represent all together at least 1% by weight,more preferably at least 2% by weight of the total liquid (under STPconditions) products exiting the conversion reactor.

According to another embodiment of the present invention, water andcarbon dioxide are also produced in the conversion reactor, and the saidwater, alcohols and ethers preferably represent together at least 50,preferably at least 80% by weight of the total liquid (under STPconditions) products exiting the conversion reactor.

According to an embodiment of the present invention, the ether(s) whichare added into the conversion reactor come directly from the organicoxygenates obtained from the conversion reactor as by-products. Saidether(s) are thus preferably separated from the alcohol(s) produced inthe conversion reactor and then recycled back into the said conversionreactor.

According to another preferred embodiment of the present invention, theether which is added to the conversion reactor is a methyl, ethyl,propyl and/or butyl ether, preferably a mixture of at least two of theseethers. Preferably the ether which is added to the conversion reactor isselected from ethanol and propanol derived ether(s) such as diethylether, n-propyl ether, ethyl n-propyl ether, ethyl isopropyl ether,n-propyl isopropyl ether and iso-propyl ether, or even more preferably amixture of at least two of these said ethers.

Quite surprisingly, the addition and/or recycle of even small amounts ofether to the conversion reactor have proven to be highly beneficial tothe alcohol(s) selectivity, particularly the ethanol selectivity, whilesimultaneously increasing catalyst activity and improving operatinglife. The addition of larger quantities of ethers has been found toconfer additional benefits of reduced water and carbon dioxideproduction.

Beyond these unexpected advantages, other advantages have also beenfound when applying the present process invention, amongst others:

(i) less waste, less by-products and thus higher carbon efficiency.

(ii) improved economics/efficiency, as there are fewer separations and areduced number of storage tanks.

As indicated, the particulate catalyst used in the conversion reactor ispreferably a modified molybdenum sulphide based catalyst and/or amodified methanol based catalyst and/or a modified Fischer-Tropschcatalyst and/or a precious metal based catalyst (e.g. rhodium).

Molybdenum sulphide based catalysts are preferred; these can be modifiedby a promoter. Promoter(s) can be added as salts during the catalystpreparation, and are preferably potassium ions (e.g. derived from a saltof potassium, such as potassium carbonate or acetate). The preferredloadings of potassium ions per molybdenum is comprised between 0.7 and1.5, most preferably between 1.0 and 1.4.

The preferred catalyst, according to the present invention, is amolybdenum sulphide based catalysts containing cobalt, the cobalt tomolybdenum molar ratio being preferably comprised between 0.5 and 3.0,more preferably between 0.5 and 1.0 and most preferably between 0.5 and0.9.

According to another embodiment of the present invention, the ether(s)added to the conversion reactor do not come from the direct recycling ofthe organic oxygenate compounds produced in the said conversion reactor.Preferably, the ether(s) come from an indirect route, e.g. from theseparation from the olefins obtained during a subsequent step of furtherchemical processing (i.e. converting the alcohols into correspondingolefins), or from a syngas to dimethyl ether process or from anetherification of methanol.

According to an embodiment of the present invention, the catalyst usedin the conversion reactor can be selected to not produce any ethercompound.

According to another embodiment of the present invention, the ethercompound added into the conversion reactor comes from the directrecycling of the organic oxygenate compounds produced in the saidconversion reactor.

According to an embodiment of the present invention, the catalyst usedin the conversion reactor can be selected to produce any ether compoundin addition to alcohols.

Any hydrocarbon-containing feed stream that can be converted into afeedstock comprising carbon monoxide and hydrogen, most preferably asynthesis gas (or “syngas”), is useful in the processes of the presentinvention. The hydrocarbon feedstock used according to the presentinvention is preferably a carbonaceous material, for example biomass,plastic, naphtha, refinery bottoms, smelter off gas, crude syngas (fromunderground coal gasification or biomass gasification), LPG, gas oil,vacuum residuals, shale oils, asphalts, various types of fuel oils,municipal waste, hydrocarbon containing process recycle streams and coaland/or natural gas; with coal and natural gas being the preferredsources and natural gas being the most preferable source.

According to a preferred embodiment of the present invention, methane isused as the hydrocarbon feedstock, to be converted into carbon oxides(s)and H2 (e.g. synthesis gas).

Processes for producing mixtures of carbon oxide(s) and hydrogen(commonly known as synthesis gas) are well known. Each method has itsadvantages and disadvantages and the choice of using a particularreforming process over another is governed by economic and availablefeed stream considerations, as well as by the desire to obtain theoptimum (H2−CO2):CO+CO2) molar ratio in the resulting synthesis gas,that is suitable for further chemical processing. The synthesis gas maybe prepared using any of the processes known in the art includingpartial oxidation of hydrocarbons, steam reforming, gas heatedreforming, microchannel reforming (as described in, for example, U.S.Pat. No. 6,284,217 which is herein incorporated by reference), plasmareforming, autothermal reforming and any combination thereof.

A discussion of these synthesis gas production technologies is providedfor in “Hydrocarbon Processing” V78, N.4, 87-90, 92-93 (April 1999)and/or “Petrole et Techniques”, N. 415, 86-93 (July-August 1998), whichare both hereby incorporated by reference.

It is also known that the synthesis gas may be obtained by catalyticpartial oxidation of hydrocarbons in a microstructured reactor asexemplified in “IMRET 3: Proceedings of the Third InternationalConference on Microreaction Technology”, Editor W Ehrfeld, SpringerVerlag, 1999, pages 187-196. Alternatively, the synthesis gas may beobtained by short contact time catalytic partial oxidation ofhydrocarbonaceous feedstocks as described in EP 0303438.

Preferably, the synthesis gas is obtained via a “Compact Reformer”process as described in “Hydrocarbon Engineering”, 2000, 5, (5), 67-69;“Hydrocarbon Processing”, 79/9, 34 (September 2000); “Today's Refinery”,15/8, 9 (August 2000); WO 99/02254; and WO 200023689.

Feedstocks comprising carbon monoxide and hydrogen, e.g., synthesis gasmay undergo purification prior to being fed to any reaction zones.Synthesis gas purification may be carried out by processes known in theart. See, for example, Weissermel, K. and Arpe H.-J., Industrial OrganicChemistry, Second, Revised and Extended Edition, 1993, pp. 19-21.

The ratio of hydrogen to carbon monoxide in the reaction zone ispreferably in the range of 20:1 to 0.1:1 by volume, more preferably inthe range of 5:1 to 0.2:1, most preferably in the range of 1.5:1 to0.5:1, e.g. 1:1. It has been found that the alcohol synthesis catalystscan also catalyse the water gas shift reaction. A consequence of this isthat hydrogen and carbon dioxide are interconvertable with carbonmonoxide and water. For high partial pressures of carbon dioxide (at orabove the water gas shift equilibrium), carbon dioxide can act as acarbon monoxide source and a hydrogen sink and this can effect theapparent preferred syngas ratio

Whilst the particular reaction conditions for the conversion reactorembodiments described hereinafter form preferred embodiments for thepresent invention, reaction conditions outside of these stated rangesare not excluded and in practice the effective reaction conditions maybe any that are sufficient to produce mainly oxygen containinghydrocarbon compounds. The exact reaction conditions will be governed bythe best compromise between achieving high catalyst selectivity,activity, lifetime and ease of operability, whilst maintaining: theintrinsic reactivity and the stability of the starting materials inquestion, as well as the desired reaction product to the reactionconditions.

In one embodiment of this invention, feedstock comprising the desiredmolar ratio of (H2−CO2):CO+CO2) is fed to a conversion reactor at acontrolled rate and the reaction is carried out in a reaction zone undercontrolled conditions of temperature and pressure in the presence of acatalyst to convert the feedstock into oxygen containing hydrocarbons.The temperature in the reaction zone is selected from the range of fromabout 150° C. to about 400° C., preferably a temperature in the range offrom about 250° C. to about 350° C. and most preferably in between 280and 320° C.

The pressure in the conversion reaction zone may be selected from therange of from about 20 to 200 bar, preferably a pressure in the range offrom about 80 to 150 bar and most preferably at between 80 and 120 bar.The hydrogen and carbon monoxide partial pressures should be sufficientto enable the production of oxygenates. The hydrogen and carbon monoxidemay be fed separately to the conversion reactor or, preferably incombination, e.g. as synthesis gas.

For purposes of this invention, GHSV is gas hourly space velocity whichis the rate of gas flow over the catalyst. It is determined by dividingthe volume of gas (at 25° C. and 1 atmosphere) which passes over thecatalyst in one hour by the volume of the catalyst.

The optimum gas hourly space velocity (GHSV) of the feedstock (liters offeedstock/hr/liter of catalyst) passing through the reaction zone canvary significantly, depending upon a variety of factors such as, forexample, reaction conditions, composition of the feedstock and quantityand type of catalyst being used. The GHSV can be maintained at any ratein the range of from about 1 to about 30,000 hr−1 or more, preferablywill be maintained at a rate of between about 500 and 20,000 hr−1, andmost preferably will be maintained at a rate of between 1,000 and 10,000hr−1.

The conversion to oxygen containing hydrocarbons (oxygenates) reactioncan be carried out in a conversion reactor by passing the mixture ofhydrogen and carbon monoxide over the conversion catalyst as a vaporphase reaction or as a liquid phase reaction, e.g. slurry reaction ortrickle bed fluidized bed reactor.

The term conversion reactor as used in the present invention pertains toany appropriate reactor, e.g. a tubular reactor using a fixed bed of thecatalyst. The reactants may be fed upwards or downwards to the catalyst,or a combination of both, to a fixed bed located in a tubular reactor.The reaction may be effected in a dynamic bed of the catalyst. In such areaction, the bed of catalyst is moving such as in the case of a fluidbed of the catalyst. The conversion reactor may preferably be chosenamongst tubular, multitubular, slurry, moving bed, fluidised bed, radialbed, multibed or reactive distillation reactor. According to anembodiment of the present invention, a fixed bed reactor is used,preferably a radial bed(s) or a multitubular vapour phase reactor or acombination thereof is used. Most preferably the conversion reactorcomprises a series of adiabatic fixed bed reactors operated either in alongitudinal and/or radial flow mode.

EXAMPLE 1 Catalyst Preparation:

A potassium promoted cobalt molybdenum sulphide catalyst was preparedaccording to example “Comparison C” given in patent number U.S. Pat. No.4,831,060, except for the sulphidation procedure which was performed asindicated below.

Catalyst Testing:

The catalyst (14.56 g; 10 ml) was loaded into a tubular down-flowreactor (15 mm internal diameter).

Gas feeds to the reactor were set to the target composition by Mass FlowControllers and the gases were premixed before entry to the top of thereactor. Liquids were introduced to the reactor via a HPLC pump set atthe target flow rate. The gas and liquid was mixed and vaporised in thepre-heat section in the reactor. The flow rates in the reactor are givenas GHSV which is defined as the volume flow of reactant gas at STP pervolume of catalyst per hour.

Prior to the reaction conditions, the catalyst was subjected to thefollowing sulphidation procedure:

1. Overnight nitrogen purge (GHSV=500 hr⁻¹) at 170 deg C.;

2. Feed changed to 2 mol % H2S in H2 stream and decrease in GHSV to 100hr⁻¹;

3. Pressure increased to 25barg;

4. Temperature increased to 250 deg C. at 1.0 deg C./min and held for 1hour;

5. Temperature further increased to 320 deg C. at 1.0 deg C./min andheld for 1 hour;

6. Decrease temperature to 270 deg C.;

7. Peed changed to 100% nitrogen at a GHSV of 2000 hr⁻¹ for purging.

After the sulphidation procedure outlined above the catalyst was broughtonto stream by changing gas feed to syngas (CO:H2 ratio of 1) and a 50ppm stream of H2S at a total GHSV of 2000 h⁻¹. The pressure wasincreased to 90Barg and then the temperature was increased (at 1.0 degC./min) to 310 deg C. The reaction products were analysed by an on-lineGas Chromatogram (CP9001-80-100 Mesh Carbosieve SII and 0.25 micronInnowax columns).

The reaction was allowed to run for 235 hours on stream under the aboveconditions. After which point a 2.5 mol % flow of methanol was fed tothe reactor. At 287 hours on stream the methanol feed liquid was changedto a methanol/diethylether mixture (90:10% w/w) and the total liquidpump rate increased such that the methanol flow rate to the reactorremained constant. The additional diethylether feed introduced to thereactor was equivalent to 0.12 mol % of the total feed rate. Productrate data from each different feed period of was averaged from 20 hoursafter the change in feed (to allow for the feed to stabilise) to the endof each period.

The results of the experiment (summarised in Table 1) demonstrate thaton addition of diethylether to the reactor feed, a clear increase in therate of ethanol production is observed. Also, the rates of higheralcohols (i.e. propanol and butanol) were observed to significantlyincrease as a result of the addition of the ether. Furthermore, usingthe feed and product rates of diethylether, the conversion of ether wasestimated to be about 60%. Within experimental error, the amount ofethanol that would be produced from the amount of converted ethercorresponds to the extra amount of ethanol seen on addition of theether.

TABLE 1 Time Average Average Average Total Average Period EthanolPropanol Butanol Alcohols C₂₋₄ Diethylether Feed (hours) Rate mg/hr Ratemg/hr Rate mg/hr Rate mg/hr Rate mg/hr No diethylether 255-286 279 36 2317 0 0.12 mol % 307-333 365 56 4 425 32 diethylether added

1. Process for the conversion of carbon oxide(s) and hydrogen containingfeedstocks to oxygen containing hydrocarbon compounds, in the presenceof a particulate catalyst comprising the step of reacting carbonoxide(s) and hydrogen in the presence of a particulate catalyst in aconversion reactor, to form products comprising oxygen containinghydrocarbon compounds; characterised in that ether(s) are added andreacted inside the conversion reactor.
 2. Process according to claim 1wherein the carbon oxide(s) and hydrogen containing feedstocks aresynthesis gas or syngas, the oxygen containing hydrocarbon compounds arealcohols, the particulate catalyst is a particulate modified molybdenumsulphide based catalyst and/or a modified methanol based catalyst and/ora modified Fischer-Tropsch catalyst and/or a precious metal (e.g.rhodium) based catalyst.
 3. Process for the conversion of hydrocarbonsto alcohols comprising the steps of a. converting a hydrocarbonfeedstock into a mixture of carbon oxide(s) and hydrogen, in a syngasreactor, b. passing the mixture of carbon oxide(s) and hydrogen from thesyngas reactor to a conversion reactor, and c. reacting said mixture insaid conversion reactor in the presence of a particulate modifiedmolybdenum sulphide based catalyst and/or a modified methanol basedcatalyst and/or a modified Pischer-Tropsch catalyst and/or a preciousmetal (e.g. rhodium) based catalyst to form alcohol(s), characterised inthat ether(s) are added into the conversion reactor.
 4. Processaccording to claim 1, wherein the ether which is added to the conversionreactor is selected from methyl, ethyl, propyl and/or butyl ether,preferably a mixture of at least two of these ethers.
 5. Processaccording to claim 4 wherein the ether is selected from ethanol andpropanol derived ether(s) such as diethyl ether, n-propyl ether, ethyln-propyl ether, ethyl isopropyl ether, n-propyl isopropyl ether andiso-propyl ether, or even preferably a mixture of at least two of theseethers.
 6. Process according to claim 4 wherein the ether is an ethylether.
 7. Process according to claim 4 wherein the ether is dimethylether.
 8. Process according to claim 1, wherein the ether(s) that areadded to the conversion reactor, come from the organic oxygenatesobtained from the conversion reactor as direct by-products.
 9. Processaccording to claim 8 wherein said ether is separated from the alcohols.10. Process according to claim 1, wherein the ether compound which isadded to the conversion reactor comes from an indirect route, e.g. fromthe separation from olefins obtained during a subsequent step ofconverting the alcohols into corresponding olefins.
 11. Use of theprocess described in claim 1, for increasing the ethanol and/or propanoland/or butanol selectivity.